KR20180112874A - Apparatus for combusting a fuel at high pressure and high temperature, and associated system - Google Patents

Abstract

A combustor arrangement is provided and includes a mixing device for mixing carbonaceous fuel with enriched oxygen and a working fluid to form a fuel mixture. The combustion chamber is at least partially defined by the porous jet member and is at least partially surrounded by the containment member. The combustion chamber has an inlet portion and an outlet portion that are longitudinally spaced apart. The fuel mixture is received by the inlet portion for combustion in the combustion chamber at a combustion temperature to form a combustion product. The combustion chamber also directs the combustion products longitudinally toward the outlet portion. Wherein said porous ejection member is substantially uniformly spaced therefrom with respect to its circumference defining said combustion chamber towards said combustion chamber to buffer the interaction between said combustion products and said porous ejection member, And is configured to guide longitudinally between the outlet portions. Related systems are also provided.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to an apparatus for burning fuel at high temperature and high pressure,

The present invention relates to devices and systems for the combustion of carbonaceous fuel with oxygen at high and high temperatures to produce combustion products containing oxygen reducing or reducing components and having an oxygen content of zero will be. One particular application relates to devices and systems for combustion of carbonaceous fuels with oxygen at high and high temperatures to produce combustion products that are oxidized to excess oxygen or contain reducing components and have an oxygen content of 0. [ One particular application may be for the generation of energy, such as electricity, through the use of a working fluid that delivers the generated energy to high-efficiency combustion of the fuel. In particular, such devices and systems may use flows such as carbon dioxide or motion fluids. In another aspect, the devices and systems may be used to generate a gas containing hydrogen and / or carbon monoxide.

While fossil fuels are expected to continue to provide the bulk of the world's electricity needs over the next 100 years, non-carbon power sources have also been developed and deployed. However, known methods for generation through fossil fuels and / or the combustion of suitable biomass are problematic due to the increased energy costs and the production of increasing emissions of carbon dioxide (CO ₂ ) and other emissions. Global warming appears to be increasing as a potentially disastrous consequence of increased carbon emissions by developed and developing countries. Solar power and wind power are not likely to replace talc fuel combustion in the near term, and nuclear power has risks associated with both diffusion and nuclear waste disposal.

Conventional devices for generation from fossil fuels or from suitable biomass are now increasingly burdened with the demand for CO ₂ capture at high pressure for delivery to underground reservoirs. However, this requirement has proven difficult to perform because current technology is only provided for very low thermal efficiencies, even though it is the best design for CO ₂ capture. Moreover, the capital cost to implement CO ₂ capture is high, resulting in significantly higher electrical costs than systems that discharge CO ₂ to the atmosphere. Accordingly, there is a continuing need in the art for devices and methods for high efficiency generation with reduced CO ₂ emissions and / or improved ease of collection and storage of the generated CO ₂ .

The oxy-fuel combustion of the carbonaceous fuels is achieved by the separation of substantially pure oxygen from the air (or otherwise providing such substantially pure oxygen for use in the combustion process) and substantially no nitrogen Involves the use of oxygen as the combustion medium to produce combustion products including carbon dioxide and water. Air and oxyfuel combustion according to the state of the art proceeds at a limited temperature and pressure to prevent excessive temperature damage to other system components such as combustor walls and / or turbine blades. The limitation of the operating temperature and / or pressure may, in some instances, undesirably increase the combustion process and / or require a relatively large combustion volume. In addition, equipment for treating the combustion process, the combustion design and / or the down-stream gas is also undesirably dependent on the propensity of the fuel utilized for the process. Moreover, due to the large volumes of combustion gases applied to conventional boiler systems in the state of the art and the release of these gases into the atmosphere, there are a number of current methods of removing contaminants from the gases of the discharge chimney, The systems are highly dependent on the detailed design of the plant and on the exact form of the fuel loaded in the plant. Each fuel type has a contrasting chemical composition and the amount of contaminants. Accordingly, current technology requires oxy-fuel combustion transformations for these exhaust gas scrubber systems or for each plant, which are designed specifically for the customer to receive a particular type of fuel with undesirable specific chemical composition.

As an example, the current technology for coal utilizes a very large single combustor with vertical tubular walls or spiral tubular walls, where high pressure steam is generated and overheated in a separate superheat zone. Combustor of the scale may suffer significant heat loss, the inside of the combustion gas in accordance with the particular coal generally used not only damaged the burner, coal ash (coal ash), slag, and SO _X, HCl, NO _X and the like due to the presence of corrosive components. These exemplary drawbacks are that the entire plant is shut down to repair or replace damaged or corroded parts and / or other components at periodic intervals, thereby reducing the utility of the plant and the loss of the plant Can lead to problems that can cause undesirable difficulties in compensating for lost output.

Other needs from the foregoing are addressed by aspects of the present invention, and in accordance with a particular aspect thereof, there is provided a fuel cell system comprising a mixing device configured to mix a carbonaceous fuel with enriched oxygen and a working fluid to form a fuel mixture A device such as a combustor device is provided.

The combustor arrangement defining a combustion chamber having an inlet portion that is longitudinally spaced from an opposing outlet portion and wherein the inlet portion is configured to receive the fuel mixture for combustion in the combustion chamber at a combustion temperature to form a combustion product do. The combustion chamber is also configured to guide the combustion product longitudinally toward the outlet portion. The combustor arrangement includes a pressure containment member and a porous perimetric transpiration member at least partially defining the combustion chamber and at least partially surrounded by the containment member. Wherein the porous ejection member is configured to substantially uniformly guide the ejected material through the porous ejection member toward the combustion chamber such that the ejected material is spirally wound about the periphery thereof to buffer the interaction between the combustion product and the porous ejection member, And is guided to flow in the longitudinal direction between the inlet portion and the outlet portion. In some embodiments, the flow of the jetted material may be guided into the combustion chamber in a substantially uniform manner about its circumference by the porous jetting member and longitudinally between the inlet portion and the outlet portion, The material is guided to flow substantially tangentially and spirally relative to the periphery of the porous jet member. The injection member may also be introduced into the combustion chamber to achieve a desired outlet temperature of the combustion product. A transformation apparatus may be configured to receive the combustion products, which convert the thermal energy associated therewith into kinetic energy in response to the combustion product.

In another aspect, the oxy-fuel combustion of the carbonaceous fuels (and / or the hydrocarbonaceous fuels) may also include the separation of substantially pure oxygen from the air (or otherwise providing such substantially pure oxygen) And the use thereof in a combustion process that produces combustion products that are substantially nitrogen free and include carbon dioxide and water. The above carbon dioxide-rich combustion products (followed by cooling and water condensation) can then be used for improved oil recovery or improved natural gas production or for disposal in suitable geological underground isolation sites (following compression and purification) And may be used for future commercial use. Operation of the oxy-fuel combustion power system at high pressure can also cause carbon dioxide derived from the fuel to be produced at high pressure, which reduces or eliminates the need to pressurize the carbon dioxide, resulting in power savings. In addition, the high pressure operation can enable refined combustion products to be used directly in the power cycle when mixed with a suitable heated operating fluid such as CO ₂ or increase. Operation of the power system at high pressure can also lead to fluid volumes of reduced volume within the power cycle, resulting in small equipment and low capital costs. The high-pressure oxy-fuel combustor with facilities for temperature control is another important aspect. Circulation (such as from a recycle stream) of suitable fluids such as combustion product gas or carbon dioxide or liquid water or vapor through the spout cooled and protected walls of the combustion chamber / space may also contribute to the regulation of the combustion temperature. The flow of the effluent stream through the combustion chamber walls may also contribute to the elimination of increased damage and / or damage to the combustion chamber walls due to thermal or ash or liquid slag intrusion effects. Thus, as part of a power system that can operate at significantly higher efficiencies and lower capital costs than current technology, it is possible to burn various types of fuels or fuel mixtures on a gas, liquid or solid basis to satisfy various requirements An efficient high-pressure, high-temperature combustor is provided. In some instances, the combustor is operable to generate a combustion product comprising hydrogen and carbon monoxide made available to subsequent needs rather than power generation.

In another aspect, the present invention provides a high-pressure, high-temperature, and high-efficacious jetting fluid for use in power generation combined with a power cycle using, for example, CO ₂ and / or H ₂ O as a working fluid Lt; RTI ID = 0.0 > and / or < / RTI > In this application, as the combustor can operate in the oxidation mode, the combustion products are thus reduced to an oxygen concentration in the range of between about 500 ppm to about 3% mole and less than about 50 ppm, preferably less than about 100 ppm moles of carbon monoxide Concentration. In another aspect, as the combustor can operate in a reducing mode, the combustion products thus have an oxygen concentration of approximately zero, and the combustion products have CO and H ₂ concentrations. The operation in the reduction mode can be configured to maximize the production of H ₂ and CO and to minimize the consumption of O ₂ . The reduction mode of operation may be advantageous not only for power generation but also for the production of H ₂ or H ₂ + CO syngas. In certain aspects, the operating pressure may range between about 40 bar to about 500 bar and preferably at least 80 bar, and the combustion product temperature may range generally between about 400 ° C and about 3500 ° C.

In aspects involving power generation, a portion of the working fluid is introduced into the combustion chamber together with the fuel and oxidant (i.e., enriched oxygen) for combustion to produce a high pressure and high temperature A fluid stream (combustion product) is generated. The working fluid may be introduced through the ejection-protected walls of the combustion chamber and / or through additional injection points for the combustion chamber. The operating fluid following mixing with the combustion products through the combustion process and the ejection may have an appropriate range (i.e., sufficiently low) temperature for introduction directly into the power plant, such as a turbine. In these examples, the total amount of working fluid introduced into the combustion chamber as a diluent for the combustion product is adjusted to provide an outlet temperature for the overall working fluid flow leaving the combustion chamber for the operating inlet temperature, the pressure of the power turbine . Advantageously, the fluid flow can maintain a relatively high pressure during expansion in the turbine, so that the pressure ratio for the turbine (i.e., the ratio of pressure at the inlet to the pressure at the outlet of the turbine) is about 12 Lt; / RTI > The fluid flow may also be further processed to separate components of the fluid flow, which may include passing the fluid flow through a heat exchanger. In particular, the expanded working fluid (at least the portion that can be recycled from the fluid stream) can pass through the same heat exchanger to heat the high-pressure working fluid before it is equally introduced into the combustor. In some aspects, the present invention provides a high pressure pure oxygen source for a power generation system that is capable of producing high efficiency power at low capital costs and producing substantially pure CO ₂ at pipeline pressure for industrial use or isolation. Thereby providing a combustor. The CO ₂ can also be recycled into the power generation system.

In other aspects, the disclosed combustion systems and methods may be configured to use a variety of fuel sources. For example, a high efficiency combustor in accordance with the present invention can be used in a gas phase (e.g., natural gas or coal derived gases), a liquid phase (e.g., hydrocarbons, bitumen) and / Pet-coke) can be used. Alternatively, other fuels such as algae, biomass or any other suitable combustible organic materials may be used, as described herein.

In another aspect, the methods and systems of the present invention, wherein the coupling system does not provide the absorption of CO ₂ in the current coal when the pipeline pressure is combined with a power system having a CO ₂ absorption-fired steam Cycle power plants can be useful in that they can exceed the best efficiency. These current power plants can, for example, provide about 45% efficiency (LHV) at 1.7-inch mercury condenser pressures, at best using bituminous coal. Aspects of the system can exceed this efficiency, for example, by delivering CO ₂ at a pressure of 200 bar.

In yet other aspects, the present invention provides the capability to use similar fuels to reduce the physical size and capital cost of the power generation system compared to current technologies. Accordingly, the methods and systems of the present invention contribute to or otherwise facilitate the construction cost associated with a significantly reduced generation system, and the relatively high efficiency of certain system combinations reduces the cost of electricity or energy production, Resulting in reduced use of fuel.

In a particular aspect, the invention relates to a power generation method comprising the use of a working fluid such as CO ₂ and / or H ₂ O. In some aspects, the method may include introducing heated and compressed CO ₂ and / or superheated steam into the fuel combustor. Preferably, the CO ₂ and / or steam may be introduced into the combustor operating at least about 80 bar. The CO ₂ and / or H ₂ O may be introduced into the combustor at two or more separate locations. Since some of the CO ₂ and / or H ₂ O can be mixed with O ₂ and solid, liquid, gaseous or supercritical fuels, the combustion temperature in the combustion chamber is determined based on the desired design value for the combustor . The remainder of the heated CO ₂ and / or superheated steam is then introduced into the combustion chamber to cool the combustion products to achieve the desired overall outlet fluid flow temperature between about 400 ° C and about 3500 ° C , Which may be required by the power generation system. Under these conditions, the CO ₂ and / or H ₂ O is the CO ₂ and / or the combustion from the combustion of the fuel gas to produce a fluid stream containing H ₂ O, more than 85 mole% purity of the desired temperature And may be mixed with an oxidizing agent such as oxygen. In the measured aspects, the outlet fluid flow temperature may be in a range between about 400 [deg.] C and about 3,500 [deg.] C. In other aspects, the outlet fluid flow may be expanded across the turbine to generate electric power (i.e., generate electricity through energy imparted to the turbine).

In some aspects, it may be useful to heat the operating fluid to a higher temperature even prior to introduction into the combustor. For example, the CO ₂ and / or H ₂ O may be heated to a temperature of at least about 200 ° C to about 700 ° C prior to introduction into the combustor. In other aspects, the CO ₂ and / or H ₂ O may be heated to a temperature between about 700 ° C. and about 1,000 ° C. prior to introduction into the combustor. In some aspects, such heating may be performed using a heat exchanger apparatus. Also, as disclosed herein, the same heat exchanger may be used to cool the fluid flow leaving the power generation turbine.

Similarly, the combustor can be usefully operated at higher pressures to produce a working fluid that can simulate very high efficiency in a power generation cycle. For example, the combustor and the introduced portion of the working fluid CO ₂ and / or H ₂ O may be pressurized to a pressure of at least about 200 bar. In other aspects, the pressure may be between about 200 bar and about 500 bar.

In some aspects, the portion of the working fluid introduced into the combustor is substantially it may be a recycled stream of pure CO ₂ any water content in the working fluid is derived from the fuel. Of course, CO ₂ from an external source can be used as the operating fluid.

The fluid flow from the combustor may include one or more other components, such as the fuel or the products of combustion derived from the combustion process, as well as the H ₂ O working fluid. The outlet fluid stream may contain components such as excess oxygen ranging from about 300 ppm to about 3% moles in addition to H ₂ O, SO ₂ , SO ₃ , NO, NO ₂ , Hg, HCl. In other aspects, the outlet fluid stream may contain varying proportions of at least H ₂ and CO and has an O ₂ content that is substantially 0.

The combustor may include an inlet nozzle device through which the fuel and the oxygen and a portion of the operating fluid are introduced into the combustor, wherein typically a desired fuel flow range between about 50% and about 100% of the design capacity The combustion is initiated and takes place in a stable manner in one of the oxidation or reduction modes. In some aspects, the operating pressure can be at least about 150 bar and at such pressure the oxygen can be combined with a fuel, such as CO ₂ and a liquid such as a natural gas or hydrocarbon distillate, Can be introduced as a mixture of phases. If at such a pressure the CO ₂ is at a temperature below about 100 ° C, the density of CO ₂ is very sufficient to be used to maintain a substantial proportion of the pulverized coal forming the slurry, Pressure combustion pump up to the combustion pressure to which the supercritical mixture of CO ₂ and oxygen is added in order to realize the required adiabatic flame temperature in the combustor. The already mixed fuel, diluent CO ₂ and oxygen should preferably be at a combined temperature lower than the auto-ignition temperature of the system. The temperature of the CO ₂ stream can be adjusted to meet these criteria. The inlet nozzle may contain an array of holes that create a fine jet of fluid in each of the injector plates causing rapid heat transfer and combustion, thereby creating a stable combustion zone. The hole sizes can range in diameter from about 0.5 mm to about 3 mm.

The walls of the combustion chamber may be aligned with a layer of porous material through which a second portion of the CO ₂ and / or H ₂ O diluent flow is directed and flowed. The flow of fluid through this porous spouted bed and optionally through additional equipment is configured to achieve the desired total outlet fluid flow outlet temperature between about 400 [deg.] C and about 3,500 [deg.] C. This flow may also contribute to cooling the ejection member to a temperature below the maximum allowable operating temperature of the material forming the cooling ejection member. The ejected material, such as the CO ₂ and / or H ₂ O diluent streams, may also cause the ingress of any liquid or solid materials or other contaminants in the fuel that may cause corrosion, odor, or otherwise damage the walls . In these examples, incident radiant heat may be radially transmitted outwardly through the porous ejection member and then radially passing through the ejection layer from the surfaces of the porous layer structure by convective heat transfer, It may be desirable to use a material for the ejection member having a reasonable (low) thermal conductivity so as to be able to be cut off. Such an arrangement is advantageous in that while the subsequent portion of the diluent flow guided through the ejection member is maintained within a range of between about 500 캜 and about 1,000 캜, while simultaneously maintaining the temperature of the porous ejecting member within the design range of the material used for this purpose Lt; / RTI > Suitable materials for the porous jet member may include, for example, porous ceramics, refractory metal fiber mats, hole-perforated cylindrical portions, and / or sintered metal layers or sintered metal powders have. Wherein the second function of the ejection member is to substantially increase the flow of the diluent ejection material to achieve a good mixing between the second portion of the diluent stream and the combustion products while enhancing the flow on the flat axis along the length of the combustion chamber To ensure flow in the longitudinal direction along the combustor as well as the inside of the flat radial form. The third function of the ejection member is to provide a buffer or otherwise prevent the solid and / or liquid particles of the ash or other contaminants in the combustion products from striking the surface of the ejection layer to cause clogging or other damage Lt; RTI ID = 0.0 > fluid. ≪ / RTI > These factors can be important, however, only when burning fuel containing residual inert non-flammable residues such as, for example, coal. The inner wall of the combustor pressure vessel surrounding the ejection member may also be insulated from the hot second diluent stream in the combustor.

Coal or other fuels with non-combustible residues can be introduced into the combustor as a slurry in water or, preferably, as a slurry in liquid CO ₂ . The liquid portion of the slurry leaves the power system at about ambient temperature and at the lowest pressure of the power cycle. In these examples, the difference in enthalpy per mole between the slurry inlet conditions and the gas outlet conditions can be about 10 kcal / gm-mol for H ₂ O and about 2.78 kcal / gm-mol for CO ₂ And provides a significantly higher efficiency for CO ₂ slurried fluids. Little additional energy is required for a high-pressure power cycle having CO ₂ as the working fluid to produce liquid CO ₂ at a temperature ranging from about -30 ° C to about 10 ° C.

The combustion temperatures of these fuels, which are generally solids such as coal, which produce incombustible residues, are preferably in the range between about 1,800 ° C and about 3,000 ° C. In these conditions, the ash or other contaminants will be in the form of liquid slag droplets originating from the fuel particles in the slurry fuel feed. These liquid slag droplets must be efficiently removed to prevent contamination of the power turbine or other subsequent processes. Removal can be accomplished using, for example, cyclone separators, impingement separators, beds of classified refractory granular filters arranged in an annular configuration, or combinations thereof . In certain aspects, the droplets can be removed from the hot working fluid by a series of cyclone separators. In order to realize efficient removal, at least two and preferably three cyclone separators are preferred. The removal efficiency can be improved by a number of factors. For example, the removal temperature can be adjusted to ensure that the slag velocity is sufficiently low to remove liquid slag that is freely discharged from the separators. The slag removal needs to be performed occasionally at an intermediate temperature between the combustion temperature and the final outlet fluid flow temperature. In such cases, the final outlet lacquer outlet temperature can be achieved by directly mixing a portion of the recycled working fluid (the ejected material) with the fluid stream leaving the slag removal system. The diameters of the cyclone separators are preferably relatively small (i.e., diameters ranging between about 20 cm to about 50 cm), while the diameter of the slag droplets should be large enough to provide good separation efficiency. These conditions can be implemented, for example, by pulverizing the coal fuel to achieve a high fraction of the particle diameter of > 50 microns. The coal is preferably microparticulated with an average particle diameter on the order of about 50 microns to about 100 microns, resulting in a final ratio of slag particles smaller than the diameter of 10 microns present in the outlet fluid stream. In some examples, the cyclone separators may follow an annular filter disposed directly upstream of the turbine.

In certain aspects, the residence time of the combustion products in the system can range from 0.2 seconds to 2 seconds for natural gas and from 0.4 seconds to 4 seconds for bituminous coal.

The fluid flow from the combustor may exhibit various different characteristics. For example, the fluid flow may comprise an oxidizing fluid. In this way, the fluid stream may comprise an oxidant (e.g., O ₂₎ (e. G. That is, burning) is rapidly oxidized by the addition of one or more components. In some aspects, the fluid flow may be a reducing fluid comprising one or more components selected from the group consisting of H ₂ , CO, CH ₄ , H ₂ S, and combinations thereof. The operation of the system in the reduction mode is substantially similar to the oxidation mode except that the proportion of the second diluent will gradually decrease as the ratio of fuel converted to H ₂ + CO increases. Also, the average residence time for the combustion products increases from about 2.5 seconds to about 4.5 seconds for natural gas as the conversion to H ₂ + CO increases, and between about 6 seconds to about 10 seconds for bituminous coal It is necessary to increase it to the range.

The foregoing aspects and other aspects will accordingly address the identified needs and provide advantages as described herein.

BRIEF DESCRIPTION OF THE DRAWINGS The present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:
BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic illustration of an ejection cooled combustor arrangement according to certain aspects of the present invention,
1A schematically illustrates a combustor temperature profile along the length of a combustion chamber in accordance with certain aspects of the present invention,
Figure 2 schematically illustrates an exemplary cross-section of a wall of a blow member in a combustor device according to certain aspects of the present invention,
2A is a schematic diagram illustrating an exemplary cross-section of a wall of a blow member in a combustor apparatus according to certain aspects of the present invention to cut a cross-section perpendicular to its longitudinal axis and to provide a spiral flow of the blow- FIG.
Figure 2b schematically illustrates an exemplary cross-section of a wall of a blow member in a combustor apparatus according to certain aspects of the present invention and illustrates an angled bore / perforation configuration to facilitate spiral flow of the blown fluid ,
Figure 2c schematically illustrates an exemplary cross-section of a wall of the ejection member in a combustor apparatus according to certain aspects of the present invention and schematically illustrating focused longitudinal strips of the ejection member to facilitate spiral flow of the ejection fluid Fig.
Figure 2D schematically illustrates a shield structure configured to be aligned / inserted with respect to the ejection member shown in Figure 2C in accordance with certain aspects of the present invention,
Figure 2e schematically illustrates a spiral flow of the ejecting fluid in the combustion chamber of a combustor device in accordance with certain aspects of the present invention,
2f is a schematic illustration of a Coanda effect that may be implemented to facilitate spiral flow of ejecting fluid in a combustion chamber of a combustor device in accordance with certain aspects of the present invention,
Figure 2G is a schematic illustration of continuously aligned, opposing helical flows of exuding fluid in a combustion chamber of a combustor device in accordance with certain aspects of the present invention,
Figures 3a and 3b are schematic illustrations of a hot fit process for a firing member assembly of a combustor device in accordance with certain aspects of the present invention,
Figure 4 schematically illustrates an apparatus for removing combustion product contaminants according to certain aspects of the present invention,
Figure 5 is a schematic diagram illustrating the trajectories of ash particles as a function of average particle size and ejection material flow rates in accordance with certain aspects of the present invention,
Figure 6 is a schematic illustration of an applicable power generation system according to certain aspects of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The invention will now be described in more detail with reference to the accompanying drawings, which, however, do not necessarily show all aspects of the invention in part. Indeed, the present invention may be embodied in many different forms and is not intended to be limited to the aspects disclosed herein. Rather, these aspects are provided to meet the legal requirements to which the present invention applies. In the drawings, like reference numerals refer to like elements.

In accordance with the present invention, one aspect of a combustor apparatus capable of operating as a solid fuel is schematically illustrated in FIG. 1, wherein the combustor apparatus is generally designated 220. In this example, the combustor device 220 may be configured to combust a solid of particulate matter, such as coal, as described herein, although other suitable combustible organic materials may also be used as fuel . The combustor arrangement 220 may be defined by a transpiration member 230 which may be configured to direct combustion fluid 222 such as ejection fluid therethrough to the combustion chamber 222 And to buffer the interaction between the combustion products and the ejection member 230 easily). Those skilled in the art will recognize that the ejection member 230 is substantially cylindrical in shape to define a substantially cylindrical combustion chamber 222 having an inlet portion 222A and an opposing outlet portion 222B. You can understand what can be done. The ejection member 230 may be at least partially surrounded by a pressure containment member 338. The inlet portion 222A of the combustion chamber 222 may be configured to receive the fuel mixture from a mixing device, According to certain aspects, the fuel mixture is combusted in the combustion chamber 222 at a specific combustion temperature to form combustion products, and the combustion chamber 222 is also directed to direct the combustion product toward the outlet portion 222B . 2) may be associated with the containment member 338 and configured to adjust its temperature. In certain instances, the heat removal apparatus 350 may include a heat transfer jacket at least partially defined by a wall 336 opposite the containment member 338, Circulation jacket 337 limited to the water-circulation jacket 337. [ In one aspect, the circulating liquid can be water.

The mixing device 250 is configured to mix the carbonaceous fuel 254 with the enriched oxygen 242 and the working fluid 236 to form the fuel mixture 200. The carbonaceous fuel 254 may be provided in the form of a solid carbonaceous fuel, a liquid carbonaceous fuel, and / or a gaseous carbonaceous fuel. The enriched oxygen 242 may be oxygen having a molarity greater than about 85%. The enriched oxygen 242 may be introduced into any of the air separation systems / systems known in the art such as, for example, a cryogenic air separation process or a high temperature ion conducting membrane separation process (from air) Technology. ≪ / RTI > The working fluid 236 may be carbon dioxide and / or water. In the examples in which the carbonaceous fuel 254 is a solid of particulate matter such as powdered coal 254A, the mixing apparatus 250 may further include the solid carbonaceous fuel 254A as the fluidizing material 255 . According to one aspect, the particulate solid carbonaceous fuel 254A may have an average particle size between about 50 microns and about 200 microns. According to another aspect, the fluidized material 255 may comprise a liquid CO ₂ having a density between the water and / or about 450㎏ / m ³ to about 1,100㎏ / m ^3. More specifically, the fluidizing material 255 may be present in association with the particulate solid carbonaceous fuel 254A, for example, from about 25% to about 95% by weight of the particulate solid carbonaceous fuel 254A, To form a slurry 250A having a range between about 25% and about 60% by weight of the particulate solid carbonaceous fuel 254A have. Although shown in FIG. 2 as being mixed with the fuel 254 and the working fluid 236 prior to introduction of the oxygen 242 into the combustion chamber 222, those skilled in the art will recognize that, It will be appreciated that the oxygen 242 may be introduced into the combustion chamber 22 as needed or separately as desired.

The mixing device 250 may be arranged on at least some of the sides so as to be spaced apart relative to the end wall 223 of the ejection member 230 associated with the inlet portion 222A of the cylindrical combustion chamber 222, (Not shown). ≪ / RTI > The injection of the fuel / fuel mixture in the combustion chamber 222 in this manner may be accomplished, for example, by injecting a large amount of the injected fuel mixture inflow stream that facilitates rapid heat transfer to the injected fuel mixture inflow stream Surface area can be provided. The temperature of the injected fuel mixture can thus rapidly rise to the ignition temperature of the fuel (i.e., the coal particles), thereby resulting in dense combustion. The jetting rate of the fuel mixture may range, for example, from about 10 m / sec to about 40 m / sec, although such values depend on many factors such as the composition of the particular jetting nozzles. Such an ejection arrangement can take many different forms. For example, the ejection arrangement may comprise, for example, arrays of holes in the diameter range of about 0.5 mm to about 3 mm, the injected fuel passing therethrough from about 10 m / s to about 40 m / s Lt; / RTI >

Direct injection " of such fuel / fuel mixture into the combustion chamber 222 directly through generally linear, linear and / or unobstructed passageways is particularly important when the fuel is a solid phase component (i.e., POX) combustors), for example, can reduce wear, corrosion and / or particulate buildup. In some instances, however, it may be advantageous for the fuel / fuel mixture to deviate from a linear, uniform flow only within the combustion chamber 222. For example, in some aspects, for example, the fuel / fuel mixture may be swirled or otherwise disturbed from the uniform flow of the straight line to enhance mixing of the fuel / fuel mixture and thus a more efficient combustion process, It may be advantageous to generate a fuel mixture.

In other aspects, the mixing device 250 may be remote or otherwise separated from the combustion chamber 222. For example, in some aspects, the mixing device 250 is configured to inject the fuel mixture 200 into the combustion chamber 222 through the containment member 338 and the ejection member 230, To the device 300, as shown in FIG. The burner device 300 may be configured to introduce the fuel / fuel mixture into the combustion chamber 222 in a substantially straight, straight flow similar to a " direct injection " device. That is, the burner device 300 receives the fuel / fuel mixture from the mixing device 250 and directs a substantially uniform linear flow of the fuel / fuel mixture to the inlet portion 222A of the combustor 222, Lt; / RTI > However, in some instances (i. E., Using fuel that does not include solid particulate), the burner apparatus 300 may be configured such that, as is well understood by those skilled in the art, / Fuel mixture may swirl or be directed into the combustion chamber 222 to induce or generate swirling. That is, the burner device 300 may be configured to swirl or otherwise disturb the uniform flow of the straight line of the fuel / fuel mixture as the fuel / fuel mixture enters the combustion chamber 222. In some aspects, the burner device 300 is configured to receive the fuel / fuel mixture from the mixing device 250 and to induce a swirling of the fuel / fuel mixture into the combustion chamber 222, Fuel mixture into the inlet portion 222A of the fuel / fuel mixture. More specifically, the burner apparatus 300 may be configured to induce a swirling of the fuel / fuel mixture on the outlet from the fuel / fuel mixture into the combustion chamber 222.

As shown in more detail in FIG. 2, the combustion chamber 222 is defined by the ejection member 230, which may be at least partially surrounded by the containment member 338. In some instances, the containment member 338 may also be partially enclosed by a heat transfer jacket 336, which cooperates with the containment member 338 to allow the low pressure water flow to circulate One or more channels 337 may be defined therebetween. Through the evaporation mechanism, the circulating water can thus be used to regulate and / or maintain the selected temperature of the fragrance containment member 338, for example, in the range of about 100 ° C to about 250 ° C. In some aspects, an insulating layer 339 may be disposed between the ejection member 230 and the containment member 338.

In some examples, the ejection member 230 may include, for example, an outer ejection member 331 and an inner ejection member 332, and the inner ejection member 332 may include the inner member 332, And the combustion chamber 222 is defined by the outer spray member 331 and the outer spray member 331. The outer firing member 331 may be comprised of any suitable high temperature-resistant material, such as steel or a steel alloy, including, for example, stainless steel and a nickel alloy. In some examples, the outer fountain member 331 includes first ejection fluid supply passages 333A extending from the surface thereof adjacent to the insulating layer 339 to the surface thereof adjacent to the ejection member 332 ). ≪ / RTI > The first ejection fluid supply passages 333A are formed in the second ejection fluid supply passages 333A defined by the containing member 338, the heat transfer jacket 336 and / or the insulating layer 339, 333B. ≪ / RTI > The first and second ejection fluid supply passages 333A and 333B may be configured to cooperatively and direct the ejection material such as ejection fluid 210 to the ejection member 332 through them. In some instances, for example, as shown in FIG. 1, the effluent fluid 210 may comprise the working fluid 236 and may be obtained from the same source in connection therewith. The first and second ejection fluid supply passages 333A and 333B can be insulated when necessary to deliver the ejection fluid 210 (i.e., CO ₂ ) with sufficient supply and sufficient pressure, 210 are directed to the combustion chamber 222 through the inner spray member 332. [ These measurements involving the ejection fluid 210 associated with the ejection member 230 can be used to determine whether the combustor apparatus 220 is operating at relatively high pressures and at relatively high temperatures Lt; / RTI >

In this regard, the inner jetting member 332 may be formed of a porous ceramic material, a perforated material, a laminate material, a porous mat composed of fibers randomly oriented in two dimensions and aligned in three dimensions, Or any other feature that exhibits the required properties as described herein, i.e., multiple flow passages or holes or other suitable openings 335 that receive and guide the ejected fluid through the inner ejection member 332. [ A suitable material, or combinations thereof. Non-limiting examples of porous ceramics and other materials suitable for such ejection cooling systems are aluminum oxide, zirconium oxide, transformation-toughened zirconium, copper, molybdenum, tungsten, copper-infiltrated, Tungsten, tungsten-coated molybdenum, tungsten-coated copper, various high temperature nickel alloys, and rhenium-sheathed or coating materials. Suitable sources of materials include, for example, CoorsTek, Inc. (Golden, CO) (zirconium); UltraMet Advanced Materials Solutions (Pacoima, CA) (refractory metal coatings); Osram Sylvania (Denver, Mass.) (Tungsten / copper); And MarkeTech International, Inc. (Port Townsend, Washington) (tungsten). Examples of perforated materials suitable for such ejection cooling systems include both materials and suppliers described above (for example, by perforating structures that are not initially porous using methods known in the art to form the perforated end structures Where it can be obtained). Examples of suitable laminate materials include both the above materials and suppliers (nonporous or partially porous structures are laminated in a manner that implements the desired end porosity using methods known in the art to yield the laminate end structures Where you can do it).

In yet other aspects, the inner jetting member 332 may extend from the inlet portion 222A of the jetting member 230 to the outlet portion 222B. In some examples, the perforated / porous structure of the inner spout member 332 may extend substantially completely (axially) from the inlet portion 222A to the outlet portion 222B, Is guided into substantially the entire length of the combustion chamber (222). That is, substantially the entirety of the inner ejection member 332 can be configured with a perforated / porous structure so that substantially the entire length of the combustion chamber 222 is ejected and cooled. More specifically, in some aspects, the cumulative perforation / hole area may be substantially the same as the surface area of the inner ejection member 332. That is, the ratio of the holes (% porosity) to the total wall area can be, for example, about 50%. In still other aspects, the perforations / holes may be spaced at an appropriate density so that a substantially uniform distribution of the ejected material from the inner ejection member 332 into the combustion chamber 222 is achieved (i.e., There is no " dead spots " where there is a lack of flow or presence of material 210). In one embodiment, the inner fountain member 332 is configured to have a diameter of 250 x 250 units per square inch to provide about 62,500 holes / in ² such that the perforations / holes are spaced about 0.004 inch (about 0.1 mm) / RTI > may include an array of perforations / holes. However, those skilled in the art will appreciate that other systems may be applicable to the configuration parameters or may be adapted to achieve desired results, such as, for example, the desired pressure drop over the flow rate across the ejection member 230 It will be appreciated that the configuration of the hole array may be varied accordingly. In another example, the pore array can be sized to vary from about 10 x 10 per square inch to about 10,000 x 10,000 per square inch with porosity percentages varying from about 10% to about 80%.

3A and 3B illustrate a structure of the combustion chamber 222 on one side of the combustor device 220. The structure of the combustion chamber 222 is similar to that of the combustion chamber 222, Quot; hot " interference fit between the enclosing structure, such as the insulating layer 339, disposed between the receiving members 338. The insulating layer 339 may be formed of a " hot " For example, in the relatively " cold " case, the ejection member 230 may be smaller, radially and / or axially dimensioned relative to the encapsulating containment member 338. As such, when inserted into the containment member 338, radial and / or axial gaps may exist between them (see, e.g., FIG. 3A). Of course, these dimensional differences may facilitate insertion of the ejection member 230 into the containment member 338. [ However, for example, when heated toward the operating temperature, the ejection member 230 may be configured to expand radially and / or axially to reduce or eliminate the above-described gaps (e.g., 3b). In this way, axial and / or radial interference fit can be formed between the ejection member 230 and the containment member 338. In the examples involving the ejection member 230 having the outer ejection member 331 and the inner ejection member 332, this forced fit can leave the inner ejection member 332 under compression. As such, suitable high temperature resistant brittle materials such as porous ceramics may be used to form the inner fountain member 332.

The spouted material 210 may be formed from the same source of carbon dioxide as the operating fluid 236 guided through the inner spouting member 332 The injected material 210 may form a buffer layer 231 (i.e., a " vapor wall ") immediately adjacent to the inner ejector member 332 in the combustion chamber 222 And the buffer layer 231 may be configured to buffer the interaction between the inner ejector member 332 and the liquefied incombustible components and the heat associated with the combustion products. That is, in some instances, the ejection fluid 210 may be transferred, for example, at least through the inner ejection member 332 at a pressure within the combustion chamber 222, The flow rate of the effluent fluid 210 (i.e., the CO ₂ flow) may be controlled at a sufficient temperature for a subsequent downstream process inlet demand (i.e., the turbine may require, for example, an inlet temperature of about 1,225 ° C.) Although it is sufficient for the blast fluid 210 to mix and cool with the combustion products to form a mixture, the outlet fluid mixture temperature is sufficient to cause slag droplets or other contaminants in the fluid or liquid state Lt; / RTI > The liquid state of the non-combustible components of the fuel can facilitate the separation of these contaminants from the combustion products in liquid form, for example, in the form of low viscosity, preferably free-flowing, Lt; RTI ID = 0.0 > damage < / RTI > Indeed, these requirements may depend on various factors such as the type of solid carbonaceous fuel (i.e. coal) used and the specific properties of the slag in the combustion process. That is, the combustion temperature in the combustion chamber 222 preferably allows any non-combustible components in the carbonaceous fuel to be liquefied in the combustion product.

The porous inner spray member 332 is configured to form a fluid shutoff wall or buffer layer 231 on the surface of the inner spray member 332 defining the combustion chamber 222, To direct the fluid / material into the combustor 222 in a radially inner manner (see, e.g., Fig. 2). The porous inner spout member 332 is configured to direct the spouting fluid into the combustion chamber 222 so that the spouting fluid 210 is directed to the inner surface of the inner spout member 332 Into the combustion chamber 222 at a substantially right angle (90 DEG). Among other advantages, the introduction of the ejected material 210 at substantially right angles to the inner ejector member 332 may be accomplished by removing slag liquid or solid droplets or other contaminants, or from the inner surface of the inner ejector member 332 The effect of directing hot combustion fluid vortices can be facilitated or otherwise improved. Reducing, minimizing or otherwise preventing contact between the slag liquid or solid droplets and the inner ejector member 332 can occur, for example, by contact between droplets / particles and solid walls Which can prevent these contaminants from fusing into larger droplets or lumps that can cause damage to the inner discharge member 332. [ The introduction of the spill material 210 at substantially right angles to the inner spill member 332 is thus directed to the inner spill member 332 having sufficient velocity or momentum to affect and damage the inner spill member 332, It is possible to facilitate or otherwise prevent the formation of combustion fluid vortices close to the jetting member 332. [

As described above, in other examples, induction of vortices into the fuel / fuel mixture along with the fuel / fuel mixture directed into the combustion chamber 222, or interference with a uniform flow of another straight line, may be advantageous. By achieving this flow disturbance after the fuel / fuel mixture has been delivered into the combustor 222, it is possible to achieve this flow disturbance prior to delivery of the fuel / fuel mixture into the nozzles or other burner devices or into the combustion chamber 222 Disadvantages associated with devices can be prevented or minimized. However, those of ordinary skill in the art will recognize that, in some instances, this post-introduction of the fuel / fuel mixture is sometimes necessary with such fuel / fuel mixture delivery devices, And / or required.

As such, in some aspects of the present invention, at least the inner spout member 332 can be configured to guide the spouting fluid 210 substantially uniformly toward the combustion chamber 222 therethrough, (331) to form the fluid barrier or buffer layer (231) against the surface of the inner firing member (332) to buffer the interaction between the member (332) and the combustion products and / 210 extend in a longitudinal direction between the inlet portion 222A and the outlet portion 222B in a spiral manner (see, for example, FIG. 2E) relative to the perimeter 221 (see FIG. 2A, for example) . More specifically, in some aspects, at least the inner fountain member 332 is configured to allow the exiting fluid 210 to be substantially uniform with respect to its circumference 221 through and into the combustion chamber 222, Is directed in the longitudinal direction between the outlet portion 222A and the outlet portion 222B so that the outlet fluid 210 is substantially tangential to the circumference 221 of the inner outlet member 332, , And are guided to flow in a helical direction (i.e., in the form of a spiral or a coil) thereto as shown in Figs. 2A and 2E. For example, the perforations / holes 335 defined by the inner firing member 332 may be tangential to the circumference of the combustion chamber 222, or otherwise along the circumference of the combustion chamber 222 Or may be arcuate or angled as it extends between its outer and inner surfaces to guide the flow of extrudate fluid 210 (see, e.g., FIG. 2A).

In another example, the holes along the longitudinal strips of the inner fountain member 332 are tangential to the circumference of the combustion chamber 222 or otherwise flow through them along the circumference of the combustion chamber 222 May be focused / closed to facilitate the ejection fluid 210 (see, e.g., Fig. 2C). In other examples, in addition to or instead of focusing the strips in the longitudinal direction of the inner fountain member 332, there may be a substantially tangential or otherwise circumferential direction along the perimeter 221 of the combustion chamber 222, A shield structure 224 (i. E., A metal or ceramic barrier device) is provided to block certain porous wall surfaces that prevent radial flow therethrough without interrupting other surfaces that facilitate the flow of the ejection fluid 210. [ Can be aligned / inserted with respect to the inner ejection member 332, for example, as shown in Fig. 2C (see Figs. 2C and 2D, for example). Although the structure 224 or the focusing process may be configured to guide the ejection fluid 210 substantially tangential to or otherwise around the perimeter 221 of the combustion chamber 222, As the flow interacts with the longitudinal combustion stream, the vector sum flow will be substantially helical. Those skilled in the art will appreciate, however, that the internal ejection of the ejection fluid 210 may be substantially tangential to the circumference 221 of the combustion chamber 222, It will be appreciated that there can be many different ways of configuring member 332. [

In another example, the perforations / holes 335 are substantially tangential to the perimeter 221 of the combustion chamber 222, or otherwise guide the percolating fluid 210 through those along the perimeter 221 To provide a coanda effect to the ejection fluid 210 that is guided through them (e.g., see FIG. 2F). In such instances, the flow of fuel / fuel mixture and / or combustion products from the inlet port portion 222A toward the outlet port portion 222B may cause the flow of the outlet fluid 210 to flow through the outlet portion 222B As well as to cause a spiral or threaded flow of the effluent fluid 210 along the combustion chamber 222. [ In these examples, the holes / perforations 335 defined by the inner spraying member 332 pass through them, for example, as shown in Fig. 2, in the longitudinal direction of the combustion chamber 222 And may extend substantially perpendicular to the axis. However, in other examples, the holes / perforations 335 may be formed in the outlet portion 222B to enhance the spiral / threaded flow mixed with the effluent fluid 210 and / or the fuel mixture / (E. G., See FIG. 2B), the holes / perforations 335 may otherwise be directed toward the fuel mixture and / or the combustion product (I. E., To enhance mixing or adjust the burn rate) to the inlet portion 222A (not shown). Thus, this manipulation of the flow of fuel mixture / combustion products along the combustion chamber 222 may, in some instances, result in a substantially straight and uniform flow of the fuel / fuel mixture into the combustor 222 Can provide a desired effect on the control of combustion characteristics and / or kinematics, without the physical device affecting the combustion of the fuel. This arrangement, i.e., the absence of physical devices to affect the fuel mixture / combustion products, can be achieved, for example, by those skilled in the art, Lt; RTI ID = 0.0 > of the < / RTI >

In this manipulation of the flow of the fuel mixture / combustion products, the burner device 300 and / or the blowing element 230 may be provided in a different position in the combustion chamber 222 in order to impart or otherwise induce their swirling in the combustion chamber 222 ≪ / RTI > For example, in one aspect, the burner apparatus 300 is configured to receive the fuel / fuel mixture from the mixing device 250 and to pump the fuel / fuel mixture into the fuel / And into the inlet portion 222A of the combustion chamber 222 in the opposite flow direction. In another aspect, the burner apparatus 300 receives the fuel / fuel mixture from the mixing apparatus 250 and directs the fuel / fuel mixture in a direction coincident with the spiral flow of the blowing fluid 210 , In the same direction) into the inlet portion 222A of the combustion chamber 222. In this way, In another aspect, the burner apparatus 300 receives the fuel / fuel mixture from the mixing apparatus 250 and directs a substantially uniform linear flow of the fuel / And the helical flow of the ejecting fluid 210 is configured to induce a vortex of the fuel / fuel mixture and / or the combustion products in the combustion chamber 222. In one embodiment,

Each such arrangement may have a separate purpose and / or effect. For example, directing the flow of the fuel / fuel mixture in a direction opposite to the spiral flow of the sparse material 210 may slow or stop the vortex in the fuel / fuel mixture due to friction between the alternating flows. . Thus, the combustion of the fuel / fuel mixture can also be delayed. Conversely, when the fuel / fuel mixture is guided in the same direction as the spiral flow of the gush fluid 210, the swirling of the fuel / fuel mixture and / or the combustion products can be improved and the fuel / It is possible to reduce the time required for substantially complete combustion as much as possible or otherwise increase the burn-up ratio of the fuel (i.e., increase the ratio of the fuel / fuel mixture to be burned during the process). Directing the fuel / fuel mixture with a substantially uniform linear flow can be achieved, for example, when the fuel / fuel mixture comprises solids or other particulates, as previously disclosed, And the desired vortex thereof can be induced by the spiral flow of the ejection member 210 to improve its combustion thereafter.

Accordingly, these effects may, in some aspects, be combined to improve the efficiency of the combustor apparatus 220. For example, as shown in FIG. 2G, the combustion chamber 222 includes a combustion section 244A disposed toward the inlet section 222A and a combustion section 242A disposed toward the outlet section 222B. A combustion zone 244B and the spout member 230 is positioned such that the spiral flow of the spout fluid 210 above the post-combustion zone 244B is directed towards the combustion zone 244A, (210) in the upper portion of the combustion zone (244A) to reverse the swirling of the combustion product induced in the post-combustion zone (244B) relative to the vortex of the fuel / fuel mixture Lt; / RTI >

In these examples, the fuel / fuel mixture is introduced into the combustion zone 244A of the combustion chamber 222 in the same direction as the spiral flow of the injection member 210 to improve its combustion, as described above . The reversal of the direction of the spiral flow of the effluent fluid 210 in the post-combustion section 244B may result in a " counter-swirl " in the combustion products, for example, , Thereby enhancing the mixing of the combustion products. In doing so, the combustion products can be mixed more quickly and completely into the outlet fluid flow from the outlet portion 222B to provide a more homogeneous outlet fluid flow.

In other aspects, in order to alternately invert the vortex of the fuel / fuel mixture and / or the combustion products induced between the inlet portion 222A and the outlet portion 222B, May be configured such that the spiral flow of the ejection fluid 210 is alternately inverted. This alternate portion of the opposing spiral flow of the ejecting fluid 210 may, for example, increase the local turbulence and thus increase the mixing of the fuel / fuel mixture and / or the combustion products have. In some instances, for example, to further increase this localized turbulence to induce the combustion kinetics, kinematics, and / or other changes in the flow path through or through the combustion chamber 222, (E. G., See FIG. 2G) extending through the at least one ejection port 246, and the at least one ejection port 246 may include at least one ejection port 246 extending therethrough as well as its flow characteristics as well as combustion kinetics and kinematics May be configured to guide the supplemental linear flow of the exuding fluid (210) into the fuel / fuel mixture and / or the combustion products to affect as much as possible. In some aspects, a suitably configured jet of ejecting fluid that is guided through the at least one laterally extending ejection port 246 may be sufficient to divide the flow in the combustion chamber 222 bifurcated , Otherwise the flow may "bend" around the jet of the ejection fluid, thereby causing the flow to be shaped along the length of the combustion chamber 222. When more than one of these ejection ports 246 is used, the ejection ports 246 may move, for example, higher temperature combustion zones to different compartments in the combustion chamber 222 To prevent the localized heating or overheating of certain compartments in the combustion chamber 222) or to induce mixing between the different combustion regions with different temperatures, angles relative to the combustion chamber 222 and / . ≪ / RTI >

In some examples, the outer firing member 331, the containment member 338, the heat transfer jacket 336, and / or the insulating layer 339 may be formed separately or in combination with respect to the firing member 332 and / To provide a " manifold " effect (i.e., to provide a substantially uniformly distributed supply) for the delivery of the ejected material / fluid 210 therethrough and into the combustion chamber 22 have. That is, a substantially uniform supply (with respect to flow rate, pressure, or any other suitable and appropriate measurements) of the effluent fluid 210 into the combustion chamber 222 may be provided to the injector member 332, The heat transfer jacket 336, and / or the insulating layer 339 to provide a uniform supply of heat to the outer spray member 331, the containment member 338, the heat transfer jacket 336, and / or the insulating layer 339, The supply of the gushing fluid 210 to the outer surface of the inner gushing member 332 may be such that a substantially uniform distribution of the gushing substance 210 in the combustion chamber 222, Can be customized and configured. This substantially uniform distribution and supply of the effluent material 210 into the combustion chamber 222 may be such that these hot combustion fluid vortices may otherwise be formed through the interaction between the unburnt fluid flow and the combustion fluid flow Which can minimize or prevent the formation of hot combustion fluid vortices, which in turn can affect or potentially damage the inner spout member 332. In some aspects, the uniformity of the distribution of the effluent material 210 within the combustion chamber 222 is preferably within at least a localized manner or frame of reference. That is, above the relatively large distances along the combustion chamber 222, the uniformity of the ejected material / fluid 210 may vary, but the fluid that can contribute to the formation of potentially damaging vortices for the flow It may be desirable and / or necessary to vary very smoothly to prevent discontinuities in the flow.

The surface of the inner blowing member 332 is also heated by the combustion products. The porous inner spray member 332 can be configured to have appropriate thermal conductivity so that the spray liquid 210 passing through the inner spray member 332 is heated while the porous inner spray member 332 ) Is cooled simultaneously, for example, in the range of about 200 DEG C to about 700 DEG C (and, in some instances, up to about 1,000 DEG C) in the region of the highest combustion temperature, The temperature of the surface of the inner ejection member 332 can be brought to a certain level. The fluid barrier wall or buffer layer 231 formed by the ejection fluid 210 cooperates with the inner ejection member 332 and thus provides an interaction between the inner ejection member 332 and the hot combustion products And the slag or other contaminant particles thus buffer the inner jet member 332 against contact, odor or other damage. It is also contemplated that in this manner, the inner ejection of the combustion product 222 may be controlled to adjust the outlet mixture of the combustion product and the ejection fluid 210 to the outlet portion 222b of the combustion chamber 222 at a temperature between about 400 [deg.] C and about 3,500 [ The ejection fluid 210 is introduced into the combustion chamber 22 through the member 332. [

Those skilled in the art will be able to determine the temperature of the combustion chamber 222 at a temperature between about 400 [deg.] C and about 3,500 < 0 > C relative to the outlet fluid portion 210 of the combustion chamber 222, It will be appreciated that the reference does not necessarily indicate that the temperature of the outlet mixture will peak at the outlet of the outlet portion 222B of the combustion chamber 222. Indeed, the combustor temperature can be adjusted, for example, as shown schematically in Figure 1A (relative temperature along the y-axis and relative position along the combustion chamber indicated along the x-axis between the inlet portion and the outlet portion) Between the outlet portion 222A of the combustion chamber 222 and the inlet portion 222B will always be able to reach a very high temperature somewhere along its length. In general, it may be desirable to obtain a sufficiently high temperature to complete the combustion process in the combustion chamber 222 sufficiently fast so that the reaction is completed before the outlet mixture exits the combustion chamber 222. After the peak temperature is obtained in the combustion chamber 222, in some instances, the temperature of the outlet mixture may be lowered by dilution from the sparging material / fluid 210.

According to some aspects, a suitable flushing fluid 210 to be implemented in the combustor arrangement 220 as described herein may be used to dilute the combustion products to produce an appropriate final outlet temperature of the operating fluid / Buffer layer 231 which may be provided with a sufficient amount and pressure of flow through the inner fountain member 332 to form the fluid barrier / In some aspects, the fluid barrier wall / buffer layer from which CO ₂ is formed thereby can be a suitable flushing fluid 210 that exhibits good insulating properties as well as desirable visible light and ultraviolet (UV) light absorbing properties. When implemented, CO ₂ is used as a supercritical fluid. Other examples of suitable blowing fluids include, for example, H ₂ O or cooled combustion product gases recycled from subsequent processes. Some fuels may be used, for example, as the beginning of the ejector fluids of the combustor apparatus to achieve appropriate operating temperatures and pressures in the combustion chamber 222 prior to injection of the fuel source during operation. Some fuels may also be used as the ejecting fluid to regulate or maintain operating temperatures and pressures of the combustor apparatus 220 during a transition between fuel sources, such as when the fuel source is changed from coal to biological. In some aspects, two or more ejection fluids may be used. The effluent fluid 210 may be optimized for the temperature and pressure conditions of the combustion chamber 222 in which the effluent fluid 210 forms the fluid barrier / buffer layer 231.

Aspects of the present invention thus provide devices and methods for producing power such as power through the use of a working fluid 236 associated with a high efficiency combustor device 220. The working fluid 236 is introduced into the combustor apparatus 220 with suitable fluids 254 and oxidant 242 and any associated materials that may be useful for efficient combustion. In certain aspects, in the implementation of the combustor device 220 configured to operate at a relatively high temperature (e.g., within a range between about 1,300 ° C and about 5,000 ° C), the working fluid 236 is directed to the combustor The fluid flow can be utilized to extract energy from it for power generation purposes as it can facilitate adjustment of the temperature of the fluid flow exiting the device 220. [

In some aspects, the blowout cooling combustor arrangement 220 may be installed in a power generation system that uses a circulating operating fluid 236, including, for example, most CO ₂ and / or H ₂ O. In a particular aspect, the working fluid 236 entering the combustor apparatus 220 preferably comprises substantially only CO ₂ . In the combustor arrangement 220 operating under oxidizing conditions, the CO ₂ working fluid 236 may include one or more components of the fuel 254, the oxidizer 242, and any products of the fuel burning process ≪ / RTI > The operating fluid 236, which may also be referred to herein as the outlet fluid, is directed toward the outlet portion 222B and exits the combustor device 220, and is shown as H ₂ O, O _2, N _2, Ar, SO _2, SO _3, NO, NO _2, HCl, with Hg and other components of small amount, which may be that the product of the combustion process (for example, material (ash) or liquefied material and Most of the CO ₂ (in the case where the working fluid is in most CO ₂ ) with a small amount of other materials, such as particulate matter or contaminants. See element 150 in FIG. The operation of the combustor arrangement 200 under reducing conditions is illustrated in Figure 1 as possible components CO ₂ , H ₂ O, H ₂ , CO, NH ₃ , H ₂ S, COS , it can lead to the exit fluid stream having a different list of possible components, including HCl, N ₂ and Ar. As discussed in more detail herein, the combustion process associated with the combustor device 220 may be regulated such that the nature of the outlet fluid flow may be reduced or oxidized, and such materials may provide particular advantages .

In certain aspects, the combustor device 220 may be configured as a high efficiency blow-out cooling combustor device capable of providing complete combustion of the fuel 254 at relatively high operating temperatures. For example, a range between about 1,300 ° C and about 5,000 ° C. This combustor arrangement 220 may, in some instances, implement one or more cooling fluids and / or one or more blowing fluids 210. With regard to the combustor arrangement 220, additional components Can also be installed. For example, an air separation unit can be provided for separating N ₂ and O ₂ , and a fuel injector unit can receive O ₂ from the air separator unit and convert the O ₂ to CO ₂ and / or H ₂ O, and And may be provided for combining with a fuel stream comprising gas, liquid, supercritical fluid, or solid phase particulate fuel slurried in a dense CO ₂ fluid.

In another aspect, the jet cooling injector device 220 may include a fuel injector for injecting pressurized fluid into the combustion chamber 222 of the combustor device 220, Vaginal fuel 254, fluidizing medium 255 (which may include the working fluid 236 as described herein), and oxygen 242. The oxygen (enriched) 242 and the CO ₂ working fluid 236 may be combined as a homogeneous supercritical mixture. The amount of oxygen present may be sufficient to combust the combustion and produce combustion products having the desired composition. The combustor arrangement 220 is also configured with a high pressure and high temperature combustion volume to receive the fuel stream as well as the ejection fluid 210 entering the combustion volume through the walls of the porous ejection member 230 defining the combustion chamber 222 And may include a combustion chamber 222. The supply amount of the blowing fluid 210 may be adjusted by adjusting the temperature of the outlet portion / turbine inlet portion of the combustor device to a desired value and / or cooling the blowing member 230 to a temperature suitable for the material forming the blowing member 230 Can be used. The ejection fluid 210 guided through the ejection member 230 provides a fluid / buffer layer on the surface of the ejection member 230 defining the combustion chamber 222 and the fluid / The particles of the ash or liquid slag derived from the spraying member 230 can be prevented from interacting with the exposed walls of the spraying member 230.

The aspects of the high-efficiency combustor arrangement may also be used for the production of various types and types of coal, wood, oil, fuel oil, natural gas, coal-based fuel gas, tar from tar sands, bitumen, , Biomass, algae, and classified combustible solid state waste wastes. In particular, coal powders or solids of particulate matter may be used. Although an exemplary coal burner apparatus 220 is disclosed herein, one of ordinary skill in the art will appreciate that the fuel used in the combustor apparatus 220 is not limited to a particular coal grade There will be. Moreover, owing to the high pressures and high temperatures maintained by the oxy-fuel combustor arrangement disclosed herein, the use of coal, bitumen (including bitumen derived from tar sands), tar, asphalt, waste tires, fuel oil, Gas derived from the gasification or pyrolysis of gasoline, jet fuel (JP-5, JP-4), natural gas, hydrocarbon material, ethanol, solid and liquid biofuels, biomass, algae, A wide variety of fuel forms can be implemented including waste. All of these fuels are suitably treated to permit injection into the combustion chamber 222 at sufficient velocities and pressures above the pressure in the combustion chamber 222. These fuels may be in the form of a liquid, slurry, gel, or paste having suitable fluidity and viscosity at ambient temperature or at elevated temperature (e.g., between about 38 ° C and about 425 ° C). Any solid fuel materials are pulverized, cut or otherwise treated to reduce the size of the particles as appropriate. Fluidized or slurried media may be added where necessary to achieve the proper configuration and to meet flow requirements for high pressure pumping. Of course, the fluidizing medium may not be required depending on the type of fuel (i.e., liquid or gas). Likewise, the circulating operating fluid may be used as the fluidizing medium, in some aspects.

In some aspects, the combustion chamber 222 is configured to sustain a combustion temperature between about 1,300 ° C and about 5,000 ° C. The combustion chamber 222 may also be configured to inject or otherwise introduce the fuel flow (and the working fluid 236) into the combustion chamber 222 at a pressure greater than the pressure at which combustion occurs. When the coal particulate is the carbonaceous fuel, the coal particles can be slurried in supercritical CO ₂ fluid or water by mixing liquid CO ₂ or water with the ground solid fuel to form a pumpable slurry . In such instances, the liquid CO ₂ is, for example, about 450㎏ / m ³ to may have a density in the range of between about 1100㎏ / m ^3, the mass fraction of said solid fuel (mass fraction) is To about 25% to about 95% (e.g., between about 25% to about 55% by weight). Alternatively, the amount of O ₂ may be mixed with the coal / CO ₂ slurry sufficiently to burn to produce the desired composition of the combustion products. Optionally, the O ₂ may be injected separately into the combustion chamber 222. The combustor arrangement 220 may include a containment member 338 at least partially surrounding the spout member 230 defining the combustion chamber 222 and an insulating member 339 may be disposed on the containment member 338, And the spraying member (230). In some instances, a heat removal device 350, such as a jacket water cooling system that defines water-circulating jackets 337, may be fastened to the containment member 338 (i.e., Quot; shell ").≪ / RTI > The ejection fluid 210 installed with the ejection member 230 of the combustor device 220 may be mixed with an inert gas such as, for example, minute quantities of H ₂ O and / or N ₂ or argon CO ₂ . The ejection member 230 may include, for example, a porous metal, a ceramic, a composite matrix, a layered manifold, any other suitable structure, or combinations thereof. In some aspects, the combustion in the combustion chamber 222 may produce high pressure and high temperature outlet fluid flow, which may subsequently be directed to a powder-producing device, such as a turbine, for its associated expansion.

1, the combustor arrangement 220 may be configured to receive the oxygen 242 at a pressure of about 355 bar. Also, the particulate solid fuel (e.g., powdered coal) 254 and the fluidizing fluid (e.g., liquid CO ₂ ) 255 may be received at a pressure of about 355 bar. Similarly, the working fluid (e.g., heated, high pressure, recyclable CO ₂ fluid) 236 may be provided at a pressure of about 355 bar and a temperature of about 835 ° C. However, according to aspects of the present invention, the fuel mixture (fuel, fluidizing fluid, oxygen, and working fluid) is received in the inlet portion 222A of the combustion chamber 222 at a pressure between about 40 bar to about 500 bar . As described herein, the relatively high pressures due to the sides of the combustor arrangement 220 can serve to concentrate the energy generated to a relatively high density with a minimum volume, and essentially a relatively high energy < RTI ID = 0.0 > It can cause density. The relatively high energy density enables subsequent processes to perform the processing of this energy in a more efficient manner relative to lower pressures, thereby providing feasible elements for the technique. Aspects of the present invention can thus provide a greater energy density (i.e., by 10-100 folds) than existing power plants. Higher energy densities improve the efficiency of the process but also reduce the cost of the equipment required to perform the energy conversion of the electric furnace from thermal energy to reduce the size and mass of the equipment and thereby reduce the cost of the equipment. .

When implemented, the CO ₂ fluidizing fluid 255, which is liquid at any pressure between the CO ₂ triple point pressure and the CO ₂ critical pressure, is approximately 55% CO ₂ and approximately 45% pulverized in mass or other mass proportions Coal is mixed with the powdered coal fuel 254 to form a mixture at a ratio of coal so that the resultant slurry can be pumped (as a fluid slurry) into the combustion chamber 222 by a suitable pump at a pressure of about 355 bar as described above have. In some aspects, the CO ₂ and the pulverized coal may be mixed at a pressure of about 13 bar prior to pumping. The O ₂ stream 242 is mixed with the recycled CO ₂ working fluid stream 236 and this combination is then mixed with the pulverized coal / CO ₂ slurry to form a single fluid mixture. The ratio of O ₂ to the coal can be sufficiently selected to complete the combustion of the coal with an additional 1% of excess O _2. In another aspect, the amount of O _2, while part of the coal are substantially uniformly oxidized with the other parts can be selected such that only partially be oxidized, it is reduced cause the fluid mixture comprising a portion H ₂ + CO + CH ₄ do. In this manner, a two stage expansion of the combustion products may be performed with some O ₂ injection and reheat between the first and second stages, as needed or desired. Also, since the fuel (coal) is only partially oxidized in the first step (i.e., the first combustion chamber at a temperature between about 400 ° C. and about 1,000 ° C.), any Are formed as solid particulates in the combustion products. For example, as the solid particulates are filtered by vortex-type and / or candle filters, the carbonaceous fuel is thereafter filtered to produce a final combustion product temperature of between about 1,300 ° C and about 3,500 ° C Can be substantially completely oxidized in the second stage (i.e., the second combustion chamber).

In other aspects, the amount of CO ₂ present in the combustion chamber 222 through the fuel mixture may range from about 1,300 ° C to about 5,000 ° C, although the combustion temperature may range from about 2,400 ° C (Adiabatic or otherwise). In one aspect, a fuel mixture of O ₂ + coal slurry + heated recycled CO ₂ is provided at a resulting temperature below the auto-ignition temperature of the fuel mixture. In order to achieve the conditions indicated, the solid carbonaceous fuel (e.g. coal) is preferably calcined by pulverizing the solid coal in a coal mill, for example, from about 50 microns to about 200 Lt; RTI ID = 0.0 > micron. ≪ / RTI > This milling process may be performed in a mill configured to provide a minimum mass ratio of particles below about 50 microns. In this manner, any nonflammable components within it that are liquefied to form liquid slag droplets in the combustion process may be greater than 10 microns in diameter. In some aspects, the fuel mixture comprising the CO ₂ + O ₂ + powdered coal slurry at a temperature of about 400 ° C may be conducted into the combustion chamber 222 at a pressure of about 355 bar, ), The net pressure at the combustion can be about 354 bar. The temperature in the combustion chamber 222 may range from about 1,300 ° C to about 5,000 ° C, and in some preferred aspects, only a single combustion step is performed.

In one example of the combustor unit (220),, 500MW net power system as described herein may be configured to operate under the following conditions in about 58% efficiency (lower heating value basis) in CH ₄ fuel.

Combustion pressure: 350 atm

Fuel inflow: 862MW

Fuel flow: 17.2 kg / s

Oxygen flow: 69.5 kg / s

CH ₄ and O ₂ are mixed with 155 kg / s of CO ₂ working fluid and burned at an adiabatic temperature of about 2,400 ° C to form an outlet fuel flow comprising CO ₂ , H ₂ O and some excess O ₂ . The combustion chamber may have an inner diameter of about 1 m and a length of about 5 m. At a temperature of about 600 캜, a flow of 395 kg / _second of CO ₂ is guided towards the jetting member of about 2.5 cm thickness and guided through the jetting member. This CO ₂ is heated to convection from the heat conducted through the ejection member which initiates from the emission of combustion in the combustion chamber to the ejection member.

With respect to the inner surface defining the combustion chamber, the surface temperature of the ejector member may be about 1,000 degrees Celsius, while the outlet fluid flow at 636.7 kilograms per second may be a temperature of about 1,350 degrees Celsius. In these examples, the average residence time for combustion and dilution of the combustion products is about 1.25 seconds. Further, the average radial inner velocity of the ejected fluid entering the combustion chamber through the ejection member is approximately 0.15 m / s.

Modifications of the examples for coal-fuel combustor devices result in a configuration with an average residence time for combustion and dilution of the combustion products in the combustion chamber of about 2.0 seconds, and a combustion chamber length of about 8 meters with an inner diameter of about 1 m. The net efficiency of the system with CO ₂ as the diluting fluid is thus about 54% (based on a lower heating value). In these examples, the radially inner velocity of the ejecting fluid may be on the order of about 0.07 m / s. Under these conditions, Figure 5 shows a schematic trajectory of a 50 micron diameter liquid slag particle projected radially outward at about 50 m / s from a distance of about 1 mm therefrom toward the jetting member. As illustrated, the particles may reach a minimum of 0.19 mm from the ejection member before returning into the exit fluid flow by the ejecting fluid through the ejection member. In these instances, the flow of the gushing fluid through the gushing member effectively buffers the interaction between the gushing member and the liquid slag particles derived from the combustion process.

Aspects of the disclosed combustor apparatus may be implemented in suitable power generation systems using related methods, as may be well understood by those skilled in the art. For example, such a power generation system may include one or more injectors that provide fuel (and optionally a flow medium), an oxidant, and a CO ₂ working fluid; And may include an ejection cooled combustor device having at least one combustion stage for burning the fuel mixture and providing outlet fluid flow as described herein. (Eg, the element 500 of FIG. 6) receives the exit fluid stream (combustion product and motion fluid), and in response to the exit fluid stream, the thermal energy associated therewith as kinetic energy The conversion device may comprise, for example, a power generation turbine having an inlet and an outlet, and power is generated as the outlet fluid flow expands. More particularly, the turbine may be configured to maintain the outlet fluid flow at a desired pressure ratio between the inlet and the outlet. A generator device (e.g., see element 550 of FIG. 6) is also configured to convert the kinetic energy of the turbine into electricity. That is, the outlet fluid flow may expand from a high pressure to a low pressure to produce an axial force that can then be converted to electric power. A heat exchanger may be provided to cool the outlet fluid flow from the turbine outlet and to heat the CO ₂ working fluid entering the combustor apparatus. One or more devices may also be provided for separating the outlet fluid stream exiting the heat exchanger into pure CO ₂ and one or more other components for recovery or disposal. This system also transmits at least a portion of the CO ₂ separated from the outlet fluid stream to compress the purified CO ₂ and the remainder as the working fluid heated by the heat exchanger into the pressurized pipeline One or more devices. However, those of ordinary skill in the art will recognize that although the present invention, in some embodiments, involves a direct implementation of the outlet fluid flow, the relatively hot outlet fluid flow may be implemented indirectly It can be understood that. That is, the outlet fluid flow can be guided into the heat exchanger, the associated thermal energy is used to heat the second working fluid stream, and the heated second working fluid stream is then transformed (e.g., , Turbine). It will also be appreciated by those of ordinary skill in the art that many other such devices may fall within the scope of the present invention.

In certain aspects of the present invention, the composition of the carbonaceous fuel may include combustible components / contaminants that may be contained in the combustible components (i. E., Contaminants) therein and which remain in the combustion products / will be. This may be the case when the carbonaceous fuel is a solid such as coal. In these aspects, a direct implementation of the outlet fluid flow may result in strengthening such non-combustible components or other damage on subsequent deformation devices (turbines) when the outlet fluid flow is directed thereto. Those of ordinary skill in the art will also appreciate that these nonflammable components are not necessarily present when other forms of carbonaceous fuel such as liquid or gaseous (i.e., natural gas) are implemented. Thus, in aspects in which direct interaction between the solid carbonaceous fuel source and the outlet fluid flow and the deformation device is realized, the power system (combustor device and converter device) is arranged between the combustor device and the converter device The separator device may further comprise a separator device. In these examples, the separator device is configured to substantially remove liquefied combustible components from the combustion products / outlet fluid stream thus received before the combustion products / outlet fluid flow is directed to the conversion device . Further, in aspects for installing the separator device, the disclosed ejection material may be introduced both before and after the separator device. More particularly, the blown material is introduced into the separator device via a transfer of the blowing member and the separator device to regulate a mixture of the blown material and the combustion products entering the separator device at or above the liquefaction temperature of the non- Can be introduced first into the combustion chamber. Following the separator device, an ejection mass transfer device (see, for example, element 475 of FIG. 6) is configured to transfer the ejected material entering the conversion device at a temperature between about 400 [deg.] C and about 3,500 [ The combustible products from which the liquefied nonflammable components have been substantially removed from leaving the separator device to control the mixture of combustible products.

As discussed above, the sides of the combustor device may have the ability to implement a combustion temperature that causes incombustible components in the solid carbonaceous fuel to be liquefied during the combustion process. In these examples, the facilities for removing the liquefied nonflammable components can be applied, for example, as a separator device 340, such as a cyclonic separator, as shown in FIG. Typically, aspects of such a cyclone separator device as embodied by the present invention include an inlet centrifuge device 100A configured to receive the combustion products / outlet fluid flow and the liquefied non-combustible components associated therewith, And an outlet centrifuge device (100B) configured to discharge the combustion products / outlet fluid flow with the liquefied nonflammable components. Each centrifuge device 100 includes a plurality of centrifugal elements or cyclones 1 that are operatively aligned in parallel relative to the central collection pipe 2 and each centrifugal element / Is configured to remove at least a portion of the liquefied incombustible components from the combustion products / exit fluid stream and to direct the removed portion of the liquefied incombustible components to a sump (20). The separator device 340 may further comprise a pressure-containing housing 125 configured to operate at elevated pressure, thereby accommodating the centrifuge device and the drainage tank. The pressure housing 125 may be an extension of the containment member 338 that also surrounds the combustor apparatus 220 or the pressurization housing 125 may be an extension of the containment member 338 that is associated with the combustor apparatus 220. [ And may be a separator member capable of fastening the containing member 338. [ In either example, due to the elevated temperature experienced by the separator device 340 via the outlet fluid flow, the pressure housing 125 also includes a heat transfer jacket (not shown) having liquid circulating therein A heat-dispersion system (not shown) operatively coupled thereto for removal of heat therefrom. In some aspects, a heat recovery device (not shown) may be operably coupled to the heat transfer jacket, wherein the heat recovery device is configured to receive liquid circulating in the heat transfer jacket and recover heat energy from the liquid .

More specifically, the (slag removal) separator device 340 shown in FIG. 4 is coupled to the combustor device 220 with respect to its outlet portion 222B to receive the outlet fluid flow / combustion products therefrom Are arranged to be continuously arranged. Wherein the ejection cooling outlet fluid flow from the combustor device 220 having droplets of the liquid slag therein (incombustible components) is passed through a conical reducer 10 to a central collector facility of the inlet centrifuge device 100A (2A). In one aspect, the separator device 340 includes three centrifugal devices 100A, 100B, and 100C (although those skilled in the art will appreciate that if the separator device is one , And may include two, three, or more centrifuge devices). In this example, the three centrifuge devices 100A, 100B, and 100C may be operably and continuously aligned to provide a three-phase cyclonic separation unit. Each centrifuge device includes, for example, a plurality of centrifuge elements (cyclones 1) arranged about the perimeter of the corresponding central collector pipe 2. The central collecting installations 2A, the central separator pipes 2 of the inlet centrifuge device 100A and the inner centrifuge device 100C are each sealed at their outlet ends. In these examples, the outlet fluid flow is directed into the branch channels 11 corresponding to each of the centrifuge elements (cyclones 1) of each centrifuge device 100. The branch channels 11 are arranged in a tangential inlet for this purpose (for example, the exit fluid flow entering the cyclone 1 causes it to interact with the walls of the cyclone 1 in a threaded flow) To tighten the inlet end of each cyclone (1). The outlet channel 3 from each cyclone 1 is then transferred into the inlet portion of the central collector pipe 2 of the corresponding centrifuge device 100. In the outlet centrifuge device 100B, the outlet fluid flow (with the non-combustible components substantially separated therefrom) flows through the collector pipe 12 and the outlet nozzle 5 into the outlet centrifuge device 100B Is guided from the central collector pipe, and a " clean " outlet fluid stream may be guided to a subsequent process, such as when it is associated with the conversion device. The exemplary three stage centrifugation apparatus can thereby reduce the slag to, for example, less than 5 ppm by mass in the outlet fluid stream.

In each step of the separator device 340 the separated liquid slag is guided from each of the cyclones 1 via outlet tubes 4 extending towards the drainage tank 20. The separated liquid slag is then guided into the pipe 14 extending from the outlet nozzle 14 or the drainage tank 20 and the pressure housing 125 for removal and / or recovery of the components therefrom. In achieving the removal of the slag, the liquid slag may be guided through a compartment having a water-cooled compartment 6 or otherwise a high pressure, cold water connection, Resulting in solidification and / or granulation of the slag. The mixture of solidified slag and water can then be separated into a slag / water fluid mixture which can be subsequently removed via a suitable pipe 9 in a vessel (collection facility) 7, (8). ≪ / RTI >

As the separator device 340 is implemented with a relatively low temperature outlet fluid flow (i.e., at a temperature sufficient to maintain the non-combustible components in a liquid form having a relatively low viscosity), in some instances, Wherein the surfaces of the separator device (340) exposed to one of the combustion products / outlet fluid flow and the liquefied non-combustible components associated therewith are configured to have at least one of high temperature resistance, high corrosion resistance and low thermal conductivity May be preferred. Examples of such materials may include zirconium oxide and aluminum oxide, although these examples are not intended to limit in any way. Thus, in certain aspects, the separator device 340 substantially removes the liquefied nonflammable components from the combustion products / outlet fluid stream and removes the nonflammable components from at least the drainage vessel 20 To maintain a low viscosity liquid form.

As described herein, the slag separation in the case of solid carbonaceous fuels is, in some instances, implemented in a single unit (separator unit 340) that can be quickly extracted from the system for maintenance and inspection . However, this aspect may provide other advantages as shown in FIG. 6, and thus the system may be easily configured to implement a " flex fuel " approach in operation with respect to the utility of a particular fuel source have. For example, the single unit separator device 340 may be configured to provide a single unit separator device 340, such that when the combustor device 220 uses solid carbonaceous fuel as the fuel source, In the system. The separator unit 340 can be removed from the system (i. E., As it may not be necessary as discussed above), if it can be preferably changed to a liquid or gaseous carbonaceous fuel source Can be guided directly to the transducer (500). The availability of the fuel may later be changed to facilitate the installation of the separator apparatus 340, as is followed by the solid carbonaceous fuel source.

Many variations and other aspects of the invention as set forth herein, including the advantages and the disclosures of the present invention as presented in the foregoing description and associated drawings, may be understood by those of ordinary skill in the art to which the invention pertains. There will be. For example, in some aspects, only a portion of the total flow of the ejected fluid material / fluid 210 into and through the inner ejector member 332 into the combustion chamber 222 is within the combustion chamber 222 Lt; RTI ID = 0.0 > spiral < / RTI > For example, up to about 90% of the total mass flow of the ejection fluid 210 entering the combustion chamber 222 can be achieved by applying a solid Or to provide or guide the spiral flow while maintaining sufficient radial flow of the ejecting fluid 210 into the combustion chamber 222 to prevent liquid particles or contaminants from affecting the fluid.

Also, in some aspects, the device 220 can be configured and aligned as, for example, a partial oxidation apparatus using the solid fuel (i.e., coal) slurry. In these examples, the partial oxidation combustor device 220 may be configured to have an operating temperature in the range of, for example, up to about 1,600 ° C, or in other instances, between about 1,400 ° C and about 1,500 ° C , The burned carbon in the fuel should be about 2% or less, preferably about 1% or less. In these examples, the relatively low operating temperature facilitates the production of H ₂ and CO by minimizing their combustion while facilitating relatively high carbon conversion and available heat.

In other aspects, the combustor device 220 may be configured to operate at a relatively high outlet temperature of about 5,000 DEG C or higher, which may, for example, facilitate dissociation of the adiabatic flame temperature or product gas Can be related to a sufficiently different temperature. For example, CO ₂ is significantly dissociated at temperatures above about 1,600 ° C.

In yet other aspects, the burner apparatus 300 may be constructed and arranged such that there is no premixing of the carbonaceous fuel and the CO ₂ component diffusing upwardly therefrom. O _{2 may} also be introduced into the burner tip, for example, into a separate set of nozzles or concentric annular rings surrounding the injection nozzle (s). In these examples, the diffusion flame can be realized for carbonaceous fuels having a high H ₂ content. Preheating of the fuel, oxygen and / or any diluents may also be required to achieve a very high temperature in the burner apparatus 300.

Accordingly, it is not intended that the invention be limited to the specific aspects disclosed, and modifications and other aspects are intended to be included within the scope of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.

Claims (23)

A combustor arrangement for defining a combustion chamber having an inlet portion that is longitudinally spaced from an opposing outlet portion, the inlet portion comprising a plurality of inlet ports for forming a fuel mixture for combustion in the combustion chamber at a combustion temperature to form a combustion product Wherein the combustion chamber is configured to receive a carbonaceous fuel, oxygen, and a working fluid, the combustion chamber configured to longitudinally direct the combustion product toward the outlet portion,
And a housing member;
A porous perimeter firing member that at least partially defines said combustion chamber and is at least partially surrounded by said containment member, said porous peripheric firing member having a perimeter extending substantially toward said combustion chamber about its perimeter, Wherein the blown material is guided substantially tangentially about its circumference to cushion the interaction between the combustion product and the surrounding porous blowing member and is helically guided about its periphery in a helical manner, Flowing in a longitudinal direction between said outlet portion and said outlet portion;
And a burner device configured to receive the carbonaceous fuel, oxygen and a working fluid and direct the fuel mixture into the combustion chamber toward the outlet portion in a helical flow direction opposite or coinciding with the spiral flow of the sparging material,
Wherein the working fluid and the ejected material comprise supercritical carbon dioxide. 2. The apparatus of claim 1, wherein the inlet portion comprises oxygen having a purity greater than about 85% with one of a solid carbonaceous fuel, a liquid carbonaceous fuel, and a gaseous carbonaceous fuel, Lt; / RTI > 2. The method of claim 1 wherein the carbonaceous fuel is a particulate solid having an average particle size of between about 50 microns and about 200 microns and the inlet portion is configured to receive the fluidizing material with the particulate carbonaceous fuel and, the fluidized material in the water and from about 450㎏ / m ³ to about 1,100㎏ / m ³ of the liquid phase has a density of including one of CO _2, and the fine particles of about 25% to about 95% by weight of solid Characterized in that the fluidizing material cooperates with the particulate solid carbonaceous fuel to form a slurry comprising the carbonaceous fuel. The apparatus of claim 1, wherein the combustion chamber is further configured to receive the carbonaceous fuel, oxygen, and operating fluid relative to the inlet portion at a pressure of about 40 bar to about 500 bar. 5. The apparatus of claim 4, wherein the combustion chamber is further configured to receive the carbonaceous fuel, oxygen, and operating fluid relative to the inlet portion at a pressure of at least about 80 bar. 2. The apparatus of claim 1, wherein the combustion temperature is between about 1,300 < 0 > C and about 5,000 < 0 > C and the combustible contaminants in the carbonaceous fuel are liquefied in the combustion chamber product. The method of claim 1, wherein the gaseous material is passed through the porous peripheric jetting member to regulate the gaseous mixture and the outlet mixture of the gaseous effluent to the outlet portion of the combustion chamber at a temperature between about 400 < 0 & And is configured to be introduced into the combustion chamber. 8. The apparatus of claim 7, wherein the gaseous substance is guided through the porous surrounding jetting member such that the gaseous substance forms a buffer layer immediately adjacent to the porous surrounding jetting member in the combustion chamber, And to buffer the interaction between liquefied nonflammable contaminants and the heat associated with the combustion products. 2. The apparatus of claim 1, wherein the porous peripheric spraying member is configured to apply a coanda effect (" spraying ") to the sprayed material guided through the combustion chamber to guide the sprayed material to flow substantially tangentially around the porous peripheric spraying member Coanda effect. ≪ / RTI > 2. The apparatus of claim 1, wherein the porous peripheric jetting member further comprises at least one jetting port extending therethrough, wherein the at least one jetting port is operatively associated with the fuel mixture and the supplementary linear Is configured to guide the flow of the fluid to affect its flow characteristics. The apparatus of claim 1, further comprising a heat removal device associated with and adapted to regulate the temperature of the containment member, the heat removal device comprising a heat transfer jacket having a liquid circulating therein. The porous peripheric spraying member according to claim 1, characterized in that the porous peripheric spraying member is further configured to define pores, the porous peripheric spraying member having a cumulative pore area that is substantially the same as the surface area of the porous peripheric spraying member . 13. The apparatus of claim 12, wherein the apertures are spaced apart and are substantially uniformly distributed between the inlet and outlet portions relative to the porous surrounding jetting member. 2. The apparatus of claim 1, further comprising a conversion device configured to receive the combustion product from the outlet portion of the combustion chamber, the conversion device being responsive to the combustion product for converting energy associated therewith into kinetic energy . 14. The apparatus of claim 13, wherein the carbonaceous fuel is solid and the apparatus further comprises a separator device disposed between the combustor device and the conversion device, wherein the separator device is operable prior to the combustion product being directed to the conversion device Is substantially configured to remove liquefied non-combustible contaminants from the combustion products contained in the combustion product. 16. The apparatus of claim 15, wherein the gaseous substance is configured to be introduced into the combustion chamber through the porous perimeter firing member to regulate a mixture of the gaseous product and the gaseous product entering the separator unit at a temperature above the liquefaction temperature of the non- Lt; / RTI > 17. The method of claim 16, further comprising the step of: subsequently placing in the separator device and substantially removing it from the separator device to regulate a mixture of the combustion product and the gushing material entering the conversion device at a temperature between about 400 & Further comprising an ejected material delivery device configured to deliver the ejected material to the combustion product comprising the liquefied non-combustible contaminants. 16. The apparatus of claim 15, wherein the separator device further comprises a plurality of successively arranged centrifuge devices, each centrifuge device having a plurality of centrifugal elements operatively aligned in parallel, Wherein the liquefied non-combustible contaminants removed from the combustion products are removably collected in a drain tank associated with the separator apparatus. 15. The method of claim 14, wherein the converting device comprises one of a turbine configured to react with the combustion product to convert energy associated therewith into kinetic energy, and a generator device configured to convert the kinetic energy into electricity Characterized in that. 2. The apparatus of claim 1, wherein the ejected material is also received by the combustion chamber as the working fluid. 2. The apparatus of claim 1 further comprising at least one fountain material source configured to provide the fountain material at the inlet portion of the combustion chamber as the operating fluid or as the fountain material to the porous peripheral fountain member Device. 2. The fuel cell of claim 1, wherein the combustion chamber includes a combustion zone disposed toward the inlet port portion and a post-combustion zone disposed toward the outlet port portion, wherein the porous surrounding jetting member comprises an induced vortex of the fuel mixture in the combustion chamber Wherein the spiral flow of the sparge material above the post-combustion section is configured to oppose the spiral flow of the sparger material above the combustion zone to invert the induced vortex of the combustion product in the post-combustion section Lt; / RTI > 2. The method of claim 1, wherein the porous peripheric sparging member comprises a spiral flow of the sparging material to alternately invert one of the fuel mixture and one induced vortex of the combustion product between the inlet portion and the outlet portion. And is configured to be alternately inverted along the section.

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